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WO2017122113A1 - Procédés de production de gaz de synthèse à partir de dioxyde de carbone - Google Patents

Procédés de production de gaz de synthèse à partir de dioxyde de carbone Download PDF

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Publication number
WO2017122113A1
WO2017122113A1 PCT/IB2017/050090 IB2017050090W WO2017122113A1 WO 2017122113 A1 WO2017122113 A1 WO 2017122113A1 IB 2017050090 W IB2017050090 W IB 2017050090W WO 2017122113 A1 WO2017122113 A1 WO 2017122113A1
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WIPO (PCT)
Prior art keywords
syngas
catalyst
carbon dioxide
feedstream
hydrogenation
Prior art date
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Ceased
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PCT/IB2017/050090
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English (en)
Inventor
Aghaddin Mamedov
Clark Rea
Jose Salazar
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SABIC Global Technologies BV
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SABIC Global Technologies BV
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Publication of WO2017122113A1 publication Critical patent/WO2017122113A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/40—Carbon monoxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/83—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/889—Manganese, technetium or rhenium
    • B01J23/8892—Manganese
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/026—Increasing the carbon monoxide content, e.g. reverse water-gas shift [RWGS]
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1076—Copper or zinc-based catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1082—Composition of support materials
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the disclosed subject matter relates to methods for producing syngas from carbon dioxide.
  • Syngas also known as synthesis gas, is primarily a mixture of carbon monoxide (CO) and hydrogen (H 2 ), but can also contain carbon dioxide (C0 2 ) and/or water (H 2 0).
  • Syngas can be a feedstock for producing higher hydrocarbons, such as fuels.
  • Syngas can also be used to produce various chemicals, including olefins, methanol, ethylene glycol, and aldehydes. In these processes, the composition of the syngas, and particularly the stoichiometric ratio of H 2 and C0 2 in the syngas, can be important in determining which materials are produced.
  • syngas can be produced from hydrocarbons, such as natural gas
  • hydrocarbons such as natural gas
  • increased concern over the environmental impact of carbon dioxide emissions has generated interest in techniques for converting carbon dioxide into syngas.
  • Certain methods for producing syngas from carbon dioxide are known in the art.
  • U.S. Patent Publication No. 2010/0190874 discloses a method for generating syngas from hydrogen and carbon dioxide, which includes contacting the feedstream with a manganese oxide catalyst containing an additional metal oxide.
  • European Patent Publication No. EP2788117 discloses a catalyst for use in the hydrogenation of carbon dioxide to produce syngas at temperatures from 400°C to 600°C.
  • the catalyst is a supported manganese oxide catalyst containing an auxiliary metal.
  • International Patent Publication No. WO2015066117 discloses a method for generating syngas over a manganese oxide catalyst that can further include another metal oxide, a support, and/or an auxiliary metal.
  • the disclosed subject matter provides novel methods for producing syngas from carbon dioxide.
  • an exemplary method of producing syngas from carbon dioxide includes contacting a feedstream comprising hydrogen and carbon dioxide with a supported metal oxide catalyst including at least one auxiliary metal to produce a product stream including syngas having a molar ratio of hydrogen to carbon monoxide (H 2 :CO) of less than 2: 1.
  • the feedstream can have a molar ratio of carbon dioxide to hydrogen (C0 2 :H 2 ) of about 1 : 1 to about 2: 1.
  • the metal oxide catalyst can include a metal selected from the group consisting of Sc, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Y, Ru, Rh, Pd, Ag, Cd, Pt, Au, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, and combinations thereof.
  • the metal oxide catalyst can include a support, for example, alumina (A1 2 0 3 ), silica (Si0 2 ), titania (Ti0 2 ), zirconia (Zr0 2 ), chromium (III) oxide (Cr 2 0 3 ), magnesia (MgO), cerium (IV) oxide (Ce0 2 ), and combinations thereof.
  • the metal oxide catalyst can include Mn/Al 2 0 3 and/or Ce/Al 2 0 3 .
  • the metal oxide catalyst can include an auxiliary metal, such as Li, Be, Na, Mg, K, Ca, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Rb, Sr, Ru, Rh, Cs, Ba, Pd, Ag, Cd, Pt, Au, and combinations thereof.
  • the auxiliary metal is Cu.
  • the catalyst includes Cu-Mn/Al 2 0 3 and/or Cu-Ce/Al 2 0 3 .
  • the method can further include hydrogenating the carbon dioxide in the feedstream to form carbon monoxide and water.
  • the hydrogenation reaction can be performed at temperatures ranging from about 600°C to about 700°C.
  • the syngas in the product stream can have a molar ratio of hydrogen to carbon monoxide (H2:CO) of about 1 : 1.
  • the method can further include separating carbon dioxide and water from the product stream.
  • the produced syngas can be used in an oxo synthesis reaction or to produce monoethylene glycol.
  • FIG. 1 depicts a method for producing syngas from carbon dioxide according to one exemplary embodiment of the disclosed subject matter.
  • the presently disclosed subject matter provides novel methods for producing syngas from carbon dioxide.
  • FIG. 1 is a schematic representation of a method for the hydrogenation of carbon dioxide to form syngas according to a non-limiting embodiment of the disclosed subject matter.
  • the method 100 can include contacting a feedstream containing carbon dioxide and hydrogen with a supported metal oxide catalyst having at least one auxiliary metal 101.
  • the feedstream can undergo a hydrogenation reaction to form a product stream 102.
  • a product stream containing syngas can be produced by the hydrogenation of carbon dioxide.
  • carbon dioxide (C0 2 ) and hydrogen (H 2 ) in the feedstream can react to form carbon monoxide (CO) and water (H 2 0) in a reverse water gas shift reaction.
  • the reverse water gas shift reaction is illustrated by:
  • the reverse water gas shift reaction is equilibrium-driven, and can be performed under conditions resulting in only partial conversion of C0 2 and H 2 .
  • the hydrogenation of carbon dioxide by the reverse water gas shift reaction can result in a product stream containing C0 2 and H 2 , as well as CO and H 2 0.
  • the ratio of H 2 and CO in the product stream can be manipulated by varying process conditions, e.g., reaction conditions, catalyst type or amount, or the ratio of C0 2 to H 2 in the feedstream.
  • the feedstream can contain C0 2 and H 2 .
  • "Feedstream” as used herein can refer to a single feedstream or multiple feedstreams, which can be combined before or during the hydrogenation reaction.
  • the feedstream can be a single mixture of H 2 or C0 2 .
  • multiple feedstreams containing H 2 and/or C0 2 can be provided.
  • the C0 2 in the feedstream can originate from various sources.
  • the C0 2 can be sourced from other chemical processes, e.g., as a waste product, or unconverted C0 2 can be recovered from the product stream and recycled to the feedstream.
  • the H 2 in the feedstream can also originate from various sources, for example from gaseous streams from other chemical processes.
  • H 2 and C0 2 can be provided in a specific ratio in the feedstream.
  • the molar ratio of C0 2 and H 2 (C0 2 :H 2 ) in the feedstream can range from about 0.5: 1 to 5: 1, e.g., about 0.5: 1, 0.6: 1, 0.7: 1, 0.8: 1, 0.9: 1, 1 : 1, 1.2: 1. 1.4: 1, 1.6: 1, 1 :8: 1, 2: 1, 3 : 1, 4: 1, or 5: 1.
  • the feedstream can contain C0 2 and H 2 in a molar ratio of about 1 : 1 to 2: 1.
  • the term “about” or “approximately” means within an acceptable error range for the particular value as determined by one of ordinary skill in the art, which will depend in part on how the value is measured or determined, i.e., the limitations of the measurement system. For example, “about” can mean a range of up to 20%, up to 10%, up to 5%), and or up to 1% of a given value.
  • the feedstream can be provided at atmospheric pressure.
  • the feedstream can be pressurized, e.g., to from about 0 bar to about 15 bar.
  • the catalyst for use in the presently disclosed methods can be any catalyst suitable for the hydrogenation of C0 2 to form CO and H 2 0.
  • the catalyst can be a supported metal oxide catalyst.
  • the catalyst can include an auxiliary metal.
  • the catalyst can include a metal oxide or a mixed metal oxide.
  • the catalyst can contain a variety of metals, including transition metals and rare earth metals.
  • the catalyst can contain Sc, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Y, Ru, Rh, Pd, Ag, Cd, Pt, Au, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, and/or combinations thereof.
  • the catalyst contains a Mn oxide and/or a Ce oxide.
  • the catalyst for use in the disclosed methods can include metal having high reduction potential.
  • coke deposits i.e., carbonaceous deposits
  • a side reaction of the hydrogenation of C0 2 is the Boudouard reaction, which is illustrated in Formula 2:
  • the Boudouard reaction can occur more frequently with higher molar ratios of C0 2 and H 2 (C0 2 :H 2 ) in the feedstream.
  • the Boudouard reaction is a redox reaction in which CO is reduced to form C0 2 and oxidized to form carbon, i.e., coke deposits, which can coat the catalyst.
  • the catalyst can be regenerated by oxidizing the coke deposits to form CO.
  • C0 2 can be used to regenerate the catalyst
  • a metal having high reduction potential i.e., a strong oxidizing agent, can be used to oxidize coke deposits.
  • the catalyst can include an auxiliary metal having high reduction potential, such as Li, Be, Na, Mg, K, Ca, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Rb, Sr, Ru, Rh, Cs, Ba, Pd, Ag, Cd, Pt, Au, and/or combinations thereof.
  • the auxiliary metal is Cu.
  • the catalyst can further include a support material.
  • the support material can be alumina (AI2O3), silica (Si0 2 ), titania (Ti0 2 ), zirconia (Zr0 2 ), chromium (III) oxide (Cr 2 0 3 ), magnesia (MgO), cerium (IV) oxide (Ce0 2 ) and/or combinations thereof.
  • the support material is alumina.
  • the catalyst can include Cu-Mn/Al 2 0 3 and/or Cu-Ce/Al 2 0 3 .
  • the catalysts of the presently disclosed subject matter can be prepared using any suitable method known in the art.
  • the catalysts can prepared by coprecipitation of the support and metal(s), or the support can be impregnated using a metal salt.
  • the catalyst can be loaded into a reactor for the hydrogenation reaction.
  • the catalyst can be within a fixed bed reactor.
  • the dimensions and structure of the reactor can vary depending on the capacity of the reactor.
  • the capacity of the reactor unit can be determined by the reaction rate, the stoichiometric quantities of the reactants and/or the feed flow rate.
  • the reactor can be operated under adiabatic or isothermal conditions.
  • the contact time for contacting the feedstream with the catalyst can depend on a number of factors including, but not limited to, the temperature, the pressure, the amount of catalyst, and the flowrate of reactants, i.e., C0 2 and H 2 , in the feedstream.
  • the feedstream can contact the catalyst for from about 1 second to about 10 minutes.
  • the reaction temperature can be a factor in determining the composition of the product stream.
  • the reaction can be maintained at a temperature from about 500°C to about 800°C, or from about 600°C to about 700°C.
  • the reaction can be maintained at a temperature from about 600°C to about 650°C.
  • the reaction can be carried out at a temperature of about 600°C, about 620°C, or about 640°C.
  • Syngas having various molar ratios of H 2 to CO can be useful for different applications.
  • syngas having a high H 2 to CO ratio e.g., greater than about 4: 1
  • Syngas having a molar ratio of H 2 to CO of about 2: 1 can be suitable for olefins synthesis.
  • Syngas having a molar ratio of H 2 to CO of less than about 2: 1 can be suitable for oxo synthesis or the production of monoethylene glycol.
  • Methods according to the presently disclosed subject matter can produce a product stream containing syngas with various molar ratios of H 2 to CO 103.
  • the product stream can contain syngas having a molar ratio of H 2 to CO of less than 3 : 1, less than 2.8: 1, less than 2.6: 1, less than 2.4: 1, less than 2.2: 1, or less than 2: 1.
  • the syngas can have a molar ratio of H 2 to CO of about 1.5: 1, 1.4: 1, 1.3 : 1, 1.2: 1, 1.1 : 1, or 1 : 1.
  • the syngas has a molar ratio of H 2 to CO of about 1 : 1.
  • C0 2 is only partially converted to CO.
  • C0 2 conversion can be from about 15% to about 50%, from about 20% to about 40%, or from about 23% to about 30%.
  • unconverted C0 2 in the product stream can be recovered and recycled to the feedstream.
  • C0 2 can be separated by an acid gas removal process.
  • H 2 0 can be separated by condensation, i.e., by cooling the product stream.
  • the product stream produced by the presently disclosed methods can include CO, H 2 , C0 2 and/or H 2 0.
  • a method can include separating at least some C0 2 and/or H 2 0 from the CO and H 2 in the product stream to produce purified syngas.
  • the syngas produced by the presently disclosed methods can be suitable for use in oxo synthesis reactions, which can alternatively be termed hydroformylation reactions. Alternatively or additionally, the syngas produced by the presently disclosed methods can be suitable for the production of monoethylene glycol.
  • the methods of the presently disclosed subject matter provide advantages over certain existing technologies for producing syngas from carbon dioxide.
  • Exemplary advantages include the hydrogenation of carbon dioxide with improved catalyst stability and the production of syngas with improved composition.
  • the methods disclosed herein provide stable catalysts for the hydrogenation of carbon dioxide to form syngas having a molar ratio of H 2 to CO of about 1 : 1, which can be suitable for downstream oxo synthesis and/or the production of monoethylene glycol.
  • the Cu/Mn-Al 2 0 3 catalyst was stable and achieved conversion of C0 2 of about 39%. Additionally, the hydrogenation reaction produced syngas with a ratio of H 2 :CO of about 2: 1.
  • Example 2 a hydrogenation reaction was performed as in Example 1, but with different flow rates of C0 2 and H 2 .
  • the hydrogenation of C0 2 was performed at a temperature of 600°C in the presence of a Cu/Mn-Al 2 0 3 catalyst.
  • the catalyst loading was 8 mL.
  • the flow rate of H 2 was 12 cc/min and the flow rate of C0 2 was 18 cc/min.
  • Table 2 displays the composition of the syngas after two and four days on stream, as well as the conversion of C0 2 and the H 2 to CO ratio of the syngas.
  • the Cu/Mn-Al 2 03 catalyst was stable and achieved conversion of C0 2 of about 30%. Additionally, the hydrogenation reaction produced syngas with a ratio of H 2 :CO of about 1.2: 1.
  • C0 2 was hydrogenated in the presence of H 2 to produce syngas.
  • the hydrogenation of C0 2 was performed at a temperature of 600°C in the presence of a Cu/Ce-Al 2 0 3 catalyst.
  • the catalyst loading was 6 mL.
  • the flow rate of H 2 was 10 cc/min and the flow rate of C0 2 was 20 cc/min.
  • Table 4 displays the composition of the syngas after two and four days on stream, as well as the conversion of C0 2 and the H 2 to CO ratio of the syngas.
  • Example 4 a hydrogenation reaction was performed as in Example 4, but at a higher temperature.
  • the hydrogenation of C0 2 was performed at a temperature of 620°C in the presence of a Cu/Ce-Al 2 03 catalyst.
  • the catalyst loading was 6 mL.
  • the flow rate of H 2 was 10 cc/min and the flow rate of C0 2 was 20 cc/min.
  • Table 5 displays the composition of the syngas after two and four days on stream, as well as the conversion of C0 2 and the H 2 to CO ratio of the syngas.
  • the Cu/Ce-Al 2 03 catalyst was stable and achieved conversion of CO 2 about 28%. Additionally, the hydrogenation reaction produced syngas with a ratio of H 2 :CO of about 1.3 : 1.
  • Example 6 a hydrogenation reaction was performed as in Examples 4 and 5, but at a higher temperature.
  • the hydrogenation of CO 2 was performed at a temperature of 640°C in the presence of a Cu/Ce-Al 2 03 catalyst.
  • the catalyst loading was 6 mL.
  • the flow rate of H 2 was 10 cc/min and the flow rate of CO 2 was 20 cc/min.
  • Table 6 displays the composition of the syngas after two and four days on stream, as well as the conversion of CO 2 and the H 2 to CO ratio of the syngas. Table 6. Composition of Example 6 syngas.
  • the Cu/Ce-Al 2 0 3 catalyst was stable and achieved conversion of C0 2 of about 30%. Additionally, the hydrogenation reaction produced syngas with a ratio of H 2 :CO of about 1.3 : 1.
  • a hydrogenation reaction was performed as in Examples 6, but with different flow rates of C0 2 and H 2 .
  • the hydrogenation of C0 2 was performed at a temperature of 640°C in the presence of a Cu/Ce-Al 2 0 3 catalyst.
  • the catalyst loading was 6 mL.
  • the flow rate of H 2 was 7.5 cc/min and the flow rate of C0 2 was 15 cc/min.
  • Table 7 displays the composition of the syngas after two and four days on stream, as well as the conversion of C0 2 and the H 2 to CO ratio of the syngas.
  • the Cu/Ce-Al 2 0 3 catalyst was stable and achieved conversion of C0 2 of about 23%. Additionally, the hydrogenation reaction produced syngas with a ratio of H 2 : CO of about 1 : 1.

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Abstract

La présente invention concerne des procédés de production de gaz de synthèse à partir de dioxyde de carbone. Les procédés peuvent consister à faire réagir un courant d'alimentation contenant de l'hydrogène et du dioxyde de carbone en présence d'un catalyseur supporté à base d'oxyde métallique comprenant au moins un métal auxiliaire pour produire le gaz de synthèse. Le gaz de synthèse peut avoir un rapport molaire hydrogène/monoxyde de carbone (H2/CO) inférieur à 2:1.
PCT/IB2017/050090 2016-01-15 2017-01-09 Procédés de production de gaz de synthèse à partir de dioxyde de carbone Ceased WO2017122113A1 (fr)

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Cited By (9)

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CN113501491A (zh) * 2021-07-20 2021-10-15 广东博大新能源科技有限公司 一种二氧化碳低温常压转化获得合成气的方法
WO2024000381A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C Procédés fischer-tropsch intégrés utilisant des catalyseurs de conversion inverse eau-gaz à l'or
WO2024000343A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C. Catalyseurs au nickel pour procédés de conversion inverse de gaz à l'eau
WO2024000370A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C Catalyseurs au manganèse pour procédés de conversion inverse de gaz à l'eau
WO2024000359A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C. Catalyseurs à base d'or pour procédés de conversion inverse de gaz à l'eau
WO2024000403A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C. Procédés fischer-tropsch intégrés utilisant du palladium et des catalyseurs de conversion eau-gaz inverse de platine
WO2024000353A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C. Procédés fischer-tropsch intégrés utilisant des catalyseurs de conversion inverse eau-gaz au manganèse
CN117623218A (zh) * 2022-08-12 2024-03-01 国家能源投资集团有限责任公司 用于二氧化碳和氢气反应制备合成气的系统及工艺
FI20235815A1 (en) * 2023-07-11 2025-01-12 Neste Oyj Catalyst, method and system for producing synthesis gas

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WO2024000343A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C. Catalyseurs au nickel pour procédés de conversion inverse de gaz à l'eau
WO2024000370A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C Catalyseurs au manganèse pour procédés de conversion inverse de gaz à l'eau
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WO2024000353A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C. Procédés fischer-tropsch intégrés utilisant des catalyseurs de conversion inverse eau-gaz au manganèse
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